Synthesis of ethyl t-butyl ether using pentasil zeolite Catalysts

Abstract: A method for synthesizing alkyl tertiary-alkyl ether which comprises reacting a C₄-C₁₀ tertiary alcohol with a C₁-C₆ primary alcohol in the presence of a catalyst comprising a pentasil zeolite having a silica/alumina ratio of 30-350, optionally in the presence of a binder consisting essentially of an oxide of an element from Group III or IV of the Periodic Table. A primary alcohol and tertiary alcohol are contacted in a molar amount of from 10:1 to 1:10 over said pentasil zeolite catalyst at a temperature of 20°C to 250°C and a pressure of 0.1 to 7.0 MPa > B. The process is suited to the production of MTBE or ETBE.

Description: This invention relates to the synthesis of alkyl t-alkyl ether using pentasil zeolite catalysts. In particular, this invention concerns an improved process for preparing ethyl tertiary butyl ether (ETBE) in one step by the reaction of tertiary butanol and ethanol in the presence of a catalyst comprising a pentasil zeolite, specifically one having a Si/Al ratio in the range 30-350 and preferably a Si/Al ratio in the range 50-150, optionally with a binder consisting essentially of an oxide from Group III or IV of the Periodic Table. The invention is especially advantageous in that the pentasil zeolites exhibit high activity during methyl t-butyl ether synthesis from methanol and t-butanol or ethyl t-butyl ether synthesis from ethanol plus t-butanol and, additionally, allow for the cosynthesis of isobutylene and diisobutylene. It is well-known that there is pressure to eliminate lead compounds from fuels for reasons of public health and environmental protection. Although the specifications for reformulated gasolines set by United States EPA will come into force in 1995, standards were brought into force in November 1992 requiring gasoline to contain at least 2.7 wt% oxygen during the winter in nonattainment areas of the U.S. If the federal air quality standard for CO was not achieved by a specified attainment date, the minimum oxygen content would increase to 3.1%. Moreover, starting in the summer of 1992, the maximum blending Reid vapor pressure (BRvp) of all gasolines was set at 0.06 MPa (9.0 psi). Since oxygenates are not only used as gasoline blending components, extenders, octane boosters and as key ingredients for reducing the emissions of CO and VOCs (Volatile Organic Compounds), it is expected that the demand for oxygenates will increase enormously in the coming years. See F. Cunill, et al., "Effect of Water Presence on Methyl tert -Butyl Ether and Ethyl tert -Butyl Ether Liquid-Phase Synthesis". IND. ENG. CHEM. RES. 1993, 32 , 564-569. Of all oxygenates, the tertiary ethers, such as methyl t-butyl ether (MTBE), ethyl tert-butyl ether (ETBE), and tert-amyl methyl ether (TAME) are preferred by refineries to lighter alcohols. They have lower blending Ried vapour pressure (BRvp), lower vaporization latent heats and low solubilities in water. The most common ether in use today is MTBE with a production of about 25 million metric tons. However, ETBE is becoming more attractive as the price of methanol goes up in relation to gasoline. It can be produced from renewable ethanol, in contrast to methanol derived from natural gas, and its use would help mitigate the greenhouse effect, Ibid., p. 564. In addition, ETBE outranks MTBE as an octane enhancer and its BRvp is only 0.03 MPa (4 psi), which makes it more attractive for BRvp blends less than 0.05 MPa (8 psi) required in some places during the summer. Therefore, a number of U.S. states and European countries are planning to make ETBE from bioethanol. At the present time, TAME, which is usually produced in MTBE refinery units when C 5 olefins are diverted into the feed, is not viewed as rivaling MTBE or ETBE. The main drawback of tertiary ethers, is that they substantially increase aldehyde emissions which are under EPA regulations and have to decrease 15% by 1995. It is believed this drawback could be largely circumvented by mixing the tertiary ethers with tertiary alcohols. Tertiary butyl alcohol (tBA) has a very low atmospheric reactivity and low aldehyde emissions, since no hydrogens are contained in the carbon link to the oxygen. It is known in the art to produce ETBE or MTBE by reacting isobutylene with either ethanol or methanol, resulting in the formation of ETBE or MTBE, respectively. The reaction normally is conducted in liquid phase with relatively mild conditions. The isobutylene can be obtained from various sources, such as naphtha cracking and catalytic cracking. The resulting reaction product stream contains the desired MTBE or ETBE, as well as unreacted isobutene and other C 4 hydrocarbons and methanol or ethanol. A number of U.S. patents, and European Published Applications of Texaco Chemical Co. disclose methods of making alkyl tertiary alkyl ethers, including MTBE and ETBE, in one step, from tert-butanol rather than isobutylene. EP-A-0333078 discloses such a reaction using a catalyst selected from acidic aluminas, acidic silica or combinations thereof and zeolites containing alumina or silica, and acidic clay mineral catalysts. Some silica-rich zeolites are disclosed in the production of MTBE. In US-A-4,822,921, to Texaco Chemical Co., there is described a method for preparing alkyl tertiary alkyl ethers which comprises reacting a C 1 -C 6 primary alcohol with a C 4 -C 10 tertiary alcohol over a catalyst comprising an inert support impregnated with phosphoric acid. US-A-5,081,318 (Texaco Chemical Co.) discloses a method for preparing alkyl tertiary alkyl ethers by reacting a C 1 -C 6 primary alcohol with a C 4 -C 10 tertiary alcohol over a catalyst comprising a fluorosulfonic acid-modified zeolite. Fluorophosphoric acid-modified zeolites are employed in EP-A-594283 (Texaco Chemical Co.) to produce alkyl tertiary alkyl ethers. Other references in the art which disclose MTBE and ETBE as products usually require two stages rather than one and use isobutylene as a reactant. For example, in US-A-4,334,890, a mixed C 4 stream containing isobutylene is reacted with aqueous ethanol to form a mixture of ethyl tertiary butyl ether (ETBE) and tertiary butyl alcohol (tBA). US-A-5,015,783 describes a process for producing ethers, including ETBE which comprises passing a feed stream to an etherification zone, passing the etherification zone effluent stream to a distillation column and further involves cooling the overhead stream, refluxing and recycling. Pentasil Zeolites The characteristic structures of catalytically important molecular sieve zeolites are discussed in "Molecular Sieve Catalysts," by J. Ward, Applied Industrial Catalysis, Vol. 3, Ch. 9, p. 271 (1984). Molecular sieve zeolites which have been investigated in most detail are those which have achieved industrial application, namely, X, Y, mordenite, the pentasil types and erionite. The pentasil family of zeolites contains a continuing series of which ZSM-5 and ZSM-11 are end members. See T. E. Whyte et al. "Zeolite Advances in the Chemical and Fuel Industries: A Technical Perspective," CATAL. REV.-SCI. ENG., 24,(4), 567-598 (1982). The article by J. W. Ward, supra , presents an excellent review of pentasil type zeolites. The pentasils usually have a Si/Al ratio greater than 10. A more detailed description of pentasil zeolites follows under the "Description of the Catalyst." A good overview of applications for zeolites, including pentasil type zeolites is found in an article titled, "Zeolite Catalysts Face Strong Industrial Future", European Chemical News, 10 July, 1989, p. 23. For example, medium pore H-ZSM-5 is sometimes added to a zeolite Y catalytic cracking catalyst to increase the aromatics content and hence motor octane, of the gasoline fraction. It has been reported in the art that methyl t-butyl ether could be prepared from isobutylene over zeolite catalysts. P. Chu et al. report results of one study in "Preparation of Methyl tert -Butyl Ether (MTBE) over Zeolite Catalysts", IND. ENG. CHEM. RES., 26 , 365 (1987). They reported that ZSM-5 and ZSM-11 have been identified to be highly selective zeolite catalysts for the preparation of MTBE from isobutylene. Compared to the conventional commercial catalyst, Amberlyst 15 resin, the pentasil zeolites are thermally stable, give no acid effluent and are less sensitive to the methanol-to-isobutene ratio. The excellent selectivity is believed to be effected by the size of their pore structure, which provides easy access to methanol and restricted access to isobutene. In contrast, small pore zeolites such as synthetic ferrierite were found inactive. Large pore zeolites, such as high-silica mordenite and zeolite Beta were not expected to exhibit shape selectivity. There is a need for the conversion of tertiary alcohols to be converted to corresponding ethers using long lasting catalysts at moderate temperatures. In particular, it would represent a distinct advance in the art if tertiary butanol, instead of isobutylene, could be converted to methyl tertiary butyl ether or ethyl tertiary butyl ether over a catalyst which exhibited extended life and good conversions at moderate temperatures. The available art does not appear to teach the use of a pentasil type zeolite for synthesis of MTBE or ETBE using t-butanol. Neither does it suggest the possibility of phase separation at temperatures greater than 160°C, nor the cosynthesis of isobutylene along with MTBE and ETBE. In accordance with certain of its aspects, the novel method of this invention for preparing alkyl tertiary-alkyl ethers, particularly ethyl tert-butyl ether (ETBE) from tertiary and primary alcohols, e.g. from tertiary butyl alcohol and ethanol in one-step comprises reacting the tertiary alcohol and primary alcohol in the presence of a catalyst comprising pentasil zeolite having a silica-to-alumina molar ratio in the range 50:1 to 150:1, optionally with a binder from Group III or IV of the Periodic Table, at an elevated temperature and moderate pressure. Typically effluent concentrations of about 41% and 28%, respectively, have been achieved and tertiary alcohol conversion (using t-butanol) levels of 68% and 59% at 120°C, respectively. The highest etherification activity is realized at 120°C. Preparation of the product of this invention may be carried out typically by reacting tertiary butyl alcohol and ethanol in the presence of a pentasil zeolite with a binder. The etherification is carried out in one-step and the catalyst comprises a pentasil zeolite having a silica/alumina ratio in the range of 50-150 with 1% to 40% Group III or IV binder. The reaction can be exemplified by the following, where R represents an ethyl group: Generally the ethanol and t-butanol coreactants may be mixed in any proportion in order to generate the desired ethyl t-butyl ether (ETBE), but preferably the molar ratio of alkanol to t-butanol (tBA) in the feed mixture should be between 10:1 and 1:10, if the yield of desired ether is to be maximized. In order to achieve maximum selectivity to ETBE, and optimum conversion per pass, an excess of methanol or ethanol in the liquid feed is desirable. The most preferred alkanol-to-tertiary butanol molar ratio is from 1:1 to 5:1. In certain circumstances, it may be particularly desirable that the tBA conversion be high enough (e.g. 60% or greater), such that the crude product mix phase separates into an isobutylene/ETBE product-rich phase and a heavier aqueous ethanol phase. The phase containing ETBE and isobutylene contains essentially no diisobutylene. Preferably such a product phase separation would be achieved at as low an etherification temperature as possible, but it is particularly observed in the range 160°-200°C. The synthesis of Eq. 1 can also be conducted where the t-butanol and ethanol reactants are mixed with certain other components including water, ketones such as acetone (Ac 2 O) and methyl ethyl ketone (MEK), peroxides and hydroperoxides such as di-t-butyl peroxide (DTBP), allyl t-butyl peroxide (ATBP), and t-butyl hydroperoxide (TBHP), as well as esters such as t-butyl formate (TBF). Typically each of said classes of components makes up less than 10% of the total feed mixture. Although not within the scope of the present invention the instant one-step process may also be applied to the preparation of other alkyl tertiary alkyl ethers. For example, said process may be applied to the reaction of a C 1 -C 6 primary alcohol (ROH in Eq. 1) such as methanol, ethanol, n-propanol and n-hexanol with a C 4 -C 10 tertiary alcohol such as, for example, tertiary butanol and tertiary amyl alcohol. Reaction of methanol with t-butanol would yield methyl tert-butyl ether (MTBE), while reaction of methanol with tertiary amyl alcohol (2-methyl-2-butanol) would then yield methyl tertiary amyl ether (TAME). Alternatively a mixture of alcohols, e.g., a mixture of C 1 -C 5 alcohols, could be reacted to give a mixture of alkyl tert-alkyl ethers. In the modified catalyst of the instant invention good results were realized using certain crystalline aluminosilicate zeolites, optionally with a binder, as catalysts for the reaction represented in Eq. 1. Particularly effective were the isostructural group of pentasil zeolites. As mentioned, Ward, supra , p. 271 provides an overview of the structure of pentasils. These zeolites, as well as silicalite have SiO 2 -Al 2 O ratios greater than 10. Silicalite, ZSM-5, ZSM-11 and related materials have structures with ten-ring channel systems in contrast with the eight-membered zeolites such as zeolite A and erionite and the twelve-membered systems such as zeolites X and Y. Pentasil zeolites are hydrophobic compared with A, X and Y zeolites. ZSM-5 has orthorhombic unit cells, whereas ZSM-11 is tetragonal. The pentasil structures are very thermal and acid stable. They are synthesized in the presence of ammonium ions, which become an integral part of the structure. Heating up to 600°C decomposes the organic cations leaving the highly porous structure. The channel size of pentasil materials is intermediate between, for example, small pore erionite and large pore zeolite Y. Hydrocarbons such as o- and m-xylene, 1,2,4-trimethylbenzene and naphthalene, with minimum diameters of about 6.9Å are absorbed slowly whereas 1,3,5-trimethylbenzene is excluded. Benzene and ρ-xylene diffuse readily in ZSM-5 whereas larger molecules such as o-xylene diffuse slowly. Highly branched paraffins diffuse much more slowly than normal and monobranched. Other ZSM series zeolites are not considered to be pentasils. ZSM-21, ZSM-35 and ZSM-38 are considered to be of the ferrierite type zeolite. ZSM-20 is considered of the faujasite type and ZSM-34 is considered to be of the offretite/erionite group. Medium pore, pentasil-type zeolites having 10-membered oxygen ring systems include, for example, ZSM-5, ZSM-11, ZSM-22, ZSM-23, ZSM-48 and laumontite. Their framework structures contain 5-membered oxygen rings and they are more siliceous than previously known zeolites. In many instances these zeolites may be synthesized with a predominance of silicon and with only a very small concentration of other atoms such as aluminum; thus, these zeolites may be considered as "silicates" with framework substitution by small quantities of other elements such as aluminum. Among the zeolites in this group, only ZSM-5 and ZSM-11 have bidirectional intersecting channels, the others have nonintersecting unidirectional channels. The medium-pore pentasils, unlike other zeolites, have pores of uniform dimension and have no large supercages with smaller size windows. This particular feature is believed to account for their unusually low coke-forming propensity in acid-catalyzed reactions. Because the pentasil zeolites are devoid of the bottle-necks in the window/cage structure, molecules larger than the size of the channel do not form with the exception perhaps at the intersections. The preferred forms of pentasil zeolite are the highly acidic, high silica forms, having silica-to-alumina mole ratio of 50:1 to 150:1 The pentasil zeolites demonstrated in the examples possess SiO 2 /Al 2 O 3 ratios of about 31:1 to ca. 350:1, and the advantage of the range 50:1 to 150:1 is seen. The instant catalysts may be formed in the presence of a binder, such as Group III or Group IV oxide, including alumina or silica. Said binders may comprise 1% to 40% of the formed catalyst. The zeolites may be combined with a binder by a variety of forming techniques. Said catalysts may be in the form of powders, pellets, granules, spheres, shapes and extrudates. The examples described herein demonstrate the advantages of using extrudates. The reaction may be carried out in either a stirred slurry reactor or in a fixed bed continuous flow reactor. The catalyst concentration should be sufficient to provide the desired catalytic effect. Etherification can generally be conducted at temperatures from 20° to 250°C; the preferred range is 80° to 200°C. Good results are observed throughout this temperature range. However, it can be noted that the best tBA conversion figures are observed when the temperature is around 140°C or higher. The total operating pressure may be from 0.1 to 7.0 MPa (0 to 1000 psig), or higher. The preferred pressure range is 0.45 to 3.5 MPa (50 to 500 psig). Typically, ETBE is generated continuously in up to ca. 40 wt% concentration or greater in the crude liquid product at total liquid hourly space velocities (LHSV) of up to 6 or higher and relatively mild conditions, where: LHSV = Volume Of Total Liquid Feed Run Through The Reactor Per Hour Volume of Catalyst In Reactor Conversions of t-butanol (tBA, wt%) are estimated in the following examples using the equation: (Mole% of tBA in Feed - Mole% of tBA in Product) Mole% of tBA in Feed x 100 The examples which follow illustrate the one-step synthesis of ETBE from tBA and EtOH using pentasil zeolites having a silica/alumina ratio of ca. 30-350, optionally with a binder, particularly in the form of extrudates. The accompanying examples illustrate: EXAMPLE 1 This examples illustrates the production of ethyl t-butyl ether from t-butanol and ethanol using a pentasil-type zeolite. Synthesis was conducted using a tubular reactor (13mm int. diam., 300 mm long) constructed of 316 stainless steel, operated upflow, and mounted in a furnace, controllable to ±1.0°C and fitted with pumps allowing flow control to <±1 cc/hr). The reactor was also fitted with a pressure regulating device and equipment for monitoring temperature, pressure and flow rate. 1) In Example 1, the cosynthesis of ETBE and isobutylene from tBA/ethanol is illustrated using ZSM-5 where the conversion levels for tBA are 59% at 120°C and 84% at 160°C (see also Table 1). 2) In Example 6, the cosynthesis of ETBE and isobutylene from tBA/ethanol is illustrated using a crude feedstock also containing sizeable quantities of water, isopropanol, acetone and methyl ethyl ketone. An extended catalyst life study with this feed has been demonstrated (see Table 6), where t-butanol conversion levels remain in the region of ca. 50% per pass and there is essentially no by-product diisobutylene (C 8 H 16 ) or diethyl ether (DEE) formation. The reactor was charged at the beginning of the experiment with 25cc of ZSM-5 zeolite having a silica/alumina ratio of 140, with 20% alumina binder, as 1.6 mm diameter extrudates. A glass wool screen was placed at the top and bottom of the reactor to ensure the catalyst would remain in the middle portion. The catalyst bed was treated with ethanol/t-butanol (1.1:1 molar mix) upflow, at a rate of 50 cc/hr, while the reactor was held at 120°C, with a total pressure of 2.07 MPa (300 psi). Samples of crude product effluent were collected periodically on stream, in 316 ss bombs and analyzed by glc. Typical analyses data for samples taken under these conditions are summarized in Table 1. Concentrations of ETBE, isobutylene, diisobutylene, alkyl ether, ethanol and t-butanol in the reaction effluent were also measured at a series of higher temperatures (140°-160°C). These data are also included in Table 5. For Sample #2, at 120°C: tBA Conversion = 59% ETBE Selectivity = 68% Isobutylene Selectivity = 24% For Sample #5, at 160°C: tBA Conversion = 84% EXAMPLE 2 Using the equipment and following the procedures of Example 1, a sample of ZSM-5 zeolite catalyst (80% zeolite, 20% alumina) was treated with a crude 1.5:1 molar mix of ethanol and t-butanol feedstock that also contains significant quantities of water, isopropanol (2-PrOH), acetone (Ac 2 O), and methyl ethyl ketone (MEK). Etherification was conducted at 120°C, 2.07 MPa (300 psi), using a LHSV of 2. Concentrations of each of these components, plus isobutylene, diisobutylene, diethyl ether (DEE) and ETBE, in the product effluents were determined by glc. Typical data are given in the accompanying Table 2. Over the period of the experiment, there were only modest changes in catalyst activity, as measured by the level of t-butanol conversion. Typical calculated conversion data are as follows: Sample 1 2 3 4 Time on Stream (Days): 1 11 17 23 t-Butanol Conversion (%): 50 49 47 43

Claims: A method for synthesizing ethyl tertiary butyl ether (ETBE) which comprises reacting tertiary butanol with ethanol in the presence of a catalyst comprising a pentasil zeolite having a silica/alumina molar ratio of 50:1 to 150:1, optionally in the presence of a binder consisting essentially of an oxide of an element from Group III or IV of the Periodic Table. A method as claimed in Claim 1, wherein the pentasil zeolite has a silica:alumina ratio of 120-150. A method as claimed in Claim 1 or 2, wherein the Group III oxide binder is alumina. A method as claimed in Claim 3, wherein the alumina comprises 1% to 40% of the formed catalyst. A method as claimed in any one of Claims 1-4, wherein the ethanol and tert-butanol are contacted in a molar amount of from 10:1 to 1:10 over said pentasil zeolite catalyst at a temperature of 20°C to 250°C and a pressure of 0.1 to 7.0 MPa. A method as claimed in anyone of Claims 2-5, wherein the operating temperature is in the range of 140°C to 200°C and the product comprises a two-phase mix of an ETBE-isobutylene product rich phase and a heavier aqueous ethanol-rich phase.

Inventors: DAI PEI-SHING EUGENE, KNIFTON JOHN FREDERICK, DAI, PEI-SHING EUGENE, KNIFTON, JOHN FREDERICK
Applicants: TEXACO CHEM INC, TEXACO CHEMICAL INC.
Application year: 1994
Main classification: C07C43
IPC codes: C07C43, C07B61, B01J29, C07C41